WO2018056735A1 - Catalyst regenerator, fluid catalytic cracking reaction system and catalyst regeneration method - Google Patents

Abstract

A catalyst regenerator according to an embodiment of the present invention comprises: a container provided with a catalyst inlet into which a coked catalyst is introduced and a catalyst outlet from which a regenerated catalyst is discharged; a first supply unit, formed below the catalyst inlet, for supplying a syngas containing solid carbon to the coked catalyst introduced into the container; and a second supply unit, formed below the first supply unit, for supplying hot air into the container.

Description

Catalyst Regenerator, Fluid Catalytic Cracking Reaction System and Catalyst Regeneration Method

The present invention relates to a catalyst regenerator, a fluid catalyst cracking reaction system, and a catalyst regeneration method, and more particularly, to continuously regenerate a coked catalyst during the process of producing olefins from refinery and naphtha separating various kinds of oil from petroleum. It relates to a catalyst regenerator, a flow catalyst cracking reaction system and a catalyst regeneration method.

In general, ethylene is a representative material of basic raw materials in petrochemical. The petrochemical process produces various materials through various processes based on olefin compounds such as ethylene and propylene.

Olefin (olefin) is obtained by decomposing naphtha (naphtha) or is obtained from ethane. In our country, mainly produced naphtha to produce olefin compounds such as ethylene.

The method for producing olefins from naphtha is conventionally performed at a high temperature of 1000 ° C. or more using a pyrolysis process (naphtha cracking center (naphtha cracking center) naphtha cracking process).

Recently, a process for producing olefins from naphtha at a lower temperature of about 700 ° C. using a catalyst has been commercialized.

In the process using a catalyst, naphtha is fed together with steam to the bottom of the riser, and the regenerated catalyst which is pushed out of the catalyst regenerator is fed back to the bottom of the riser, and the naphtha is mixed with the naphtha and the catalyst to rise up the riser Decomposes to produce olefins. The catalyst is coked by cracking naphtha in the riser. That is, carbon particles cover the surface of the catalyst.

The riser is connected to a cyclone provided on top of the catalyst regenerator. The olefin gas thus formed is separated in the cyclone and exited from the stripper vessel and sent to the FCC (fluid catalytic cracking) main column, and the caulked catalyst is separated from the cyclone and falls down. Fuel gas is supplied to the waste heat boiler.

The conventional pyrolysis process also uses a catalyst. At this time, naphtha decomposes at a high temperature to generate a considerable amount of coke around 7% of the weight of the catalyst. That is, carbon particles cover the surface of the catalyst.

The caulked catalyst must be recycled, sent back to the riser, mixed with naphtha and subjected to a cycle used for the decomposition reaction of naphtha. However, when the catalyst is coked, it is difficult for the decomposition reaction of naphtha to be smooth. Thus, the caulked catalyst dropped to the bottom of the catalyst regenerator is regenerated. In other words, regeneration burns off coke attached to the catalyst.

When the amount of catalyst used is high, the catalyst forms a fluidized bed type with a high density. That is, the catalyst is accumulated in the center wall provided at the lower end of the stand pipe to guide the catalyst. In order to prevent this, hot air and steam are injected toward the catalyst falling from the inner lower side of the center wall together with the fuel for catalyst regeneration. Hot air and steam injected upwards assist in catalyst regeneration and at the same time prevent the catalyst fluidized bed from increasing in density.

Such a catalyst regenerator is not suitable for application to a catalyst regenerator having a low amount of catalyst. In other words, a catalyst regenerator for regenerating a heavy catalyst has a stand pipe and a center wall therein, and requires a configuration for supplying hot air and steam to the inside of the center wall.

One aspect of the present invention is a catalyst regenerator, a flow catalyst cracking to continuously regenerate the coked catalyst in a simple configuration when the amount of the catalyst is small during the process of producing olefins from the refinery and naphtha to separate various types of oil from petroleum It is to provide a reaction system, and a catalyst regeneration method.

The catalyst regenerator according to an embodiment of the present invention is formed in a vessel having a catalyst inlet through which a coked catalyst is introduced and a catalyst outlet through which the regenerated catalyst is discharged, and formed below the catalyst inlet, and a caulked catalyst introduced into the container. And a first supply unit for supplying a synthesis gas containing solid carbon to the second supply unit, and a second supply unit formed below the first supply unit and supplying hot air into the container.

The catalyst inlet can be disposed above the vessel and the catalyst outlet can be disposed below the vessel.

The first supply unit may include a first nozzle assembly for supplying the syngas, and the second supply unit may include a second nozzle assembly for supplying the hot air.

The second nozzle assembly is spaced apart from the first nozzle assembly by a first distance L1, spaced apart from the catalyst outlet by a second distance L2, and the first distance L1 is a flow rate of the caulked catalyst. (Vc) can be set (L1 = Vc * Tm) to the product size of the coking catalyst and the time Tm at which the hot syngas can be mixed.

The vessel may set a caulking volume corresponding to the first distance L1, and the caulking volume may be set to a size that allows the caulked catalyst to be additionally caulked by syngas.

The second distance (L2) is set to the product size of the flow rate (Vcc) of the additionally coked catalyst and the time (Tb) that the additionally coked catalyst can be burned by the synthesis gas (L2 = Vcc * Tb) Can be.

The vessel sets a combustion volume corresponding to the second distance L2, and the combustion volume may be set to a size capable of further burning the coked catalyst with hot air.

The first nozzle assembly includes a first donut tube corresponding to a horizontal cross-sectional shape of the cylinder of the container, and a first supply tube installed in the container and connected to the first donut tube to supply a synthesis gas. The first donut tube body may include a first mixed gas nozzle and a second mixed gas nozzle that form a spraying direction at an angle set to 90 degrees or less with respect to a reference line passing through a center in the vertical direction in a circular cross section in the vertical direction.

The second nozzle assembly includes a second donut tube corresponding to the horizontal cross-sectional shape of the cylinder of the container, and a second supply tube installed in the container and connected to the second donut tube to supply hot air. The second donut tube may include a first air nozzle and a second air nozzle forming an injection direction at an angle set to 90 degrees or less with respect to a reference line passing through a center in the vertical direction in a circular cross section in the vertical direction.

The first supply unit may be connected to a plasma burner that forms a rotating arc to generate syngas through a partial oxidation reaction.

At least one of the first supply unit and the second supply unit may include a supply pipe connected to an outer circumferential side of the container.

At least one of the first supply unit and the second supply unit may include a supply chamber formed along an outer periphery of the container and connected to a supply port formed in the container, and a supply pipe externally connected to the supply chamber. .

The catalyst inlet can be disposed above the vessel and the catalyst outlet can be disposed laterally of the vessel.

The catalyst inlet may include a plurality of catalyst pipes arranged long downward in the interior of the vessel to guide the inflow of the caulked catalyst, and the catalyst outlet may be formed at a position higher than a lower end of the catalyst pipe.

The first supply portion may be formed on the side of the vessel at a position lower than the lower end of the catalyst pipe, and the second supply portion may be formed below the vessel at a position lower than the first supply portion.

In the fluidized catalyst cracking reaction system according to an embodiment of the present invention, a reaction part causing decomposition reaction by mixing a catalyst with petroleum or naphtha, and a separation part separating the reaction product generated in the reaction part from the catalyst according to the properties and characteristics And the catalyst regenerator regenerating the caulked catalyst introduced from the separation unit and supplying the catalyst to the reaction unit.

Catalyst regeneration method according to an embodiment of the present invention, the catalyst supply step of supplying a coked catalyst, an additional coking step of further coking the coked catalyst with a high temperature synthesis gas, a regeneration step of regenerating the additional coked catalyst, and An evacuation step of evacuating the regenerated catalyst.

The catalyst supplying step may supply the coked catalyst from a fluid catalytic cracking (FCC) reaction system.

The additional coking step may be further coked by feeding hot syngas containing solid carbon to the coked catalyst.

The regeneration step may supply hot air to regenerate the additional coked catalyst.

The caulked catalyst supplied in the catalyst feeding step may pass through the further coking step, the regeneration step, and the discharge step while moving from the top to the bottom.

One embodiment of the present invention, the first and second supply unit (first, second nozzle assembly) is provided in the interior of the container in order, in the fluid catalytic cracking (FCC (fluid catalytic cracking)) reaction system, Since the high temperature synthesis gas containing the solid carbon and the hot air are sequentially supplied to the catalyst, it is possible to additionally coke the continuously coked catalyst and to regenerate the coked catalyst.

1 is a cross-sectional view of a catalyst regenerator according to a first embodiment of the present invention.

FIG. 2 is a diagram illustrating an operation of supplying a high temperature syngas containing solid carbon to a coked catalyst in the first nozzle assembly of FIG. 1.

3 is a bottom view of the first nozzle assembly shown in FIG. 2.

FIG. 4 is a diagram illustrating an operation of supplying hot air to a mixture of hot syngas and a caulked catalyst formed under the first nozzle assembly in the second nozzle assembly of FIG. 1.

5 is a cross-sectional view of the (first, second) supply unit applied to the catalyst regenerator according to the second embodiment of the present invention.

6 is a cross-sectional view of the (first, second) supply unit applied to the catalyst regenerator according to the third embodiment of the present invention.

7 is a sectional view of a catalyst regenerator according to a fourth embodiment of the present invention.

8 is a block diagram of a flow catalyst cracking reaction system according to an embodiment of the present invention.

9 is a flowchart of a catalyst regeneration method according to an embodiment of the present invention.

Hereinafter, exemplary embodiments of the present invention will be described in detail with reference to the accompanying drawings so that those skilled in the art may easily implement the present invention. As those skilled in the art would realize, the described embodiments may be modified in various different ways, all without departing from the spirit or scope of the present invention.

In the drawings, parts irrelevant to the description are omitted in order to clearly describe the present invention, and like reference numerals designate like elements throughout the specification.

In addition, since the size and thickness of each component shown in the drawings are arbitrarily shown for convenience of description, the present invention is not necessarily limited to the illustrated.

Throughout the specification, when a part is "connected" to another part, it includes not only "directly connected", but also "indirectly connected" between other members. In addition, when a part is said to "include" a certain component, this means that it may further include other components, except to exclude other components unless otherwise stated.

When a part of a layer, a film, an area, a plate, etc. in the specification is said to be "on" or "on" another part, it is not only when it is "right on" the other part but also when there is another part in the middle. Include. And "on the (up)" means to be located above or below the target portion, and does not necessarily mean to be located above the gravity direction.

For example, in the process of producing a reaction product (eg, olefin) by decomposing a target material (eg, naphtha) by using a catalyst, the reaction unit (eg, an overheated target material injected with steam) Naphtha) and a high temperature catalyst are mixed to cause decomposition reaction of the target material (eg naphtha). The target material (eg naphtha) continues to catalyze and decompose as it rises along the reaction section.

A separation unit (eg cyclone) separates the caulked catalyst sent from the reaction unit and the resulting reaction product (eg olefin). The separated reaction product (eg olefin) is sent to the main column (not shown) of the FCC in a fluid catalytic cracking (FCC) reaction system, and the coked catalyst is regenerated off into a catalyst regenerator.

1 is a cross-sectional view of a catalyst regenerator according to a first embodiment of the present invention. For convenience, Figure 1 will be described by taking the cracked naphtha, after the regeneration of the caulked catalyst as an example. Carbon or carbon and gaseous HC are supplied in a gaseous flow through the catalyst regenerator 1 so as to be deposited or coked on the catalyst, and separately supplied with an oxidant (combustion air) to coking. The burned carbon is then burned to compensate for the reduced flow temperature during the decomposition reaction and to regenerate the catalyst.

Referring to FIG. 1, the catalyst regenerator 1 of the first embodiment is configured to regenerate a caulked catalyst introduced after a naphtha decomposition reaction, and the vessel 30 through which the caulked catalyst flows, the interior of the vessel 30. And a first supply part (for example, a first nozzle assembly) 10 and a second supply part (for example, a second nozzle assembly) 20 to be installed therein.

The vessel 30 has a catalyst inlet 31 above and a catalyst outlet 32 below. As an example, the container 30 may be formed in a cylindrical body. The caulked catalyst produced by the decomposition reaction of naphtha in the riser is introduced into the upper portion of the vessel 30 through the catalyst inlet 31, is regenerated downward from the interior of the vessel 30, and then discharged to the catalyst outlet 32. .

The vessel 30 has a distributor 33 above via the catalyst inlet 31. The distributor 33 uniformly distributes the caulked catalyst introduced through the catalyst inlet 31 and falling from above to the bottom in the horizontal direction of the vessel 30. Thus, the caulked catalyst via the distributor 33 may fall into a uniform distribution in the horizontal direction toward the first supply, that is, the first nozzle assembly 10.

In other words, for the continuous flow of the catalyst caulked in the interior of the vessel 30, the first nozzle assembly 10 is installed below the catalyst inlet 31 and the distributor 33, the second nozzle assembly 20 It is installed below the first nozzle assembly 10. The catalyst outlet 32 is provided below the second nozzle assembly 20.

The first nozzle assembly 10 sprays and supplies a high temperature syngas containing solid carbon to the caulked catalyst. That is, the first nozzle assembly 10 may supply carbon or carbon and HC, and may be supplied through partial oxidation of fuel. The second nozzle assembly 20 supplies hot air to the mixture of the coked catalyst and the hot syngas via the first nozzle assembly 10.

The first nozzle assembly 10 and the second nozzle assembly 20 are spaced apart at a first distance L1. The first distance L1 is set to be equal to or more than a distance at which the coked catalyst passed through the first nozzle assembly 10 and the high temperature syngas injected from the first nozzle assembly 10 are sufficiently mixed. For example, the first distance L1 may be set as a product of the flow rate Vc of the caulked catalyst and the time Tm at which the caulked catalyst and the high temperature syngas are mixed.

The container 30 sets the caulking volume corresponding to the first distance L1. The caulking volume in the vessel 30 is set in the flow direction of the caulked catalyst to a size that allows the caulked catalyst to be further caulked by the hot syngas supplied from the first nozzle assembly 10. .

The second nozzle assembly 20 and the catalyst outlet 32 are spaced apart by a second distance L2. The second distance L2 is set to be equal to or more than a distance for sufficiently burning the catalyst further coked through the first distance L1 with the hot air injected from the second nozzle assembly 20. For example, the second distance L2 is set to a product of or equal to the product of the flow rate Vcc of the additionally coked catalyst and the time Tb at which the additionally coked catalyst can be combusted by the syngas. .

The container 30 sets the combustion volume corresponding to the second distance L2. The combustion volume in the vessel 30 is set to a size capable of further burning the coked catalyst with hot air, thereby further burning the coked catalyst with the hot air supplied from the second nozzle assembly 20. It is set to a size that allows it.

FIG. 2 is an operating state diagram of supplying a high temperature syngas containing solid carbon to a coked catalyst in the first nozzle assembly of FIG. 1, and FIG. 3 is a view of the first nozzle assembly of FIG. 2. Bottom view.

1 to 3, the first nozzle assembly 10 is disposed above the inside of the container 30 to provide solid carbon to the caulked catalyst C1 flowing out from the catalyst inlet 31. It is configured to supply a hot syngas containing.

The first nozzle assembly 10 is connected to a partial oxidation burner 40. Partial oxidation burner 40 is configured to produce hot gases containing solid carbon, ie syngas (partial oxidation product).

For example, the partial oxidation burner 40 may be formed as a plasma burner that partially oxidizes hydrocarbon fuel oil. Although not shown, the plasma burner includes an electrode to which a high voltage is applied, a ground electrode forming a discharge gap with the high voltage electrode, and an oxidant supply part and a fuel supply part supplying an oxidant (air) and fuel to cause a discharge between the electrode and the ground electrode. For example, a nozzle). In addition, the plasma burner may form a rotation arc by forming the supply direction of the oxidant (air) in the rotation direction.

In general, a complete oxidation reaction that completely burns hydrocarbon-based fuels produces water and carbon dioxide. However, if the amount of oxygen is supplied insufficiently than complete combustion, partial oxidation reaction occurs incompletely.

Partial oxidation reactions produce hydrogen, carbon monoxide, low carbon number hydrocarbons, solid carbon, carbon dioxide, and water. In this way, the partial oxidation burner 40 generates a high temperature synthesis gas containing solid carbon by plasma reaction by the supplied hydrocarbon fuel and air.

A typical burner can achieve partial oxidation within the combustible range of very limited air-fuel ratios. However, when a typical burner is applied to a partial oxidation burner, solid carbon can be produced and supplied only within a limited flammable range (that is, when the temperature is relatively high).

In contrast, when the plasma burner is applied to the partial oxidation burner 40, the partial oxidation burner 40 may generate and supply solid carbon in a combustible range having a very wide air-fuel ratio. In addition, the partial oxidation burner 40 can maintain the partial oxidation reaction while controlling the amount of solid carbon generated.

In other words, partial oxidation with low air-fuel ratio generates a large amount of hydrogen and solid carbon, and partial oxidation (close to complete combustion) with high air-fuel ratio produces a higher amount of hydrogen and solid carbon with higher temperature.

In general, when the air-fuel ratio increases in the low air-fuel ratio section, when the temperature of the synthesis gas generated and discharged from the partial oxidation burner 40, that is, the partial oxidation product increases, and the air-fuel ratio increases after the highest temperature, the partial oxidation burner 40 The temperature of the syngas generated and supplied at) decreases.

The first nozzle assembly 10 includes a first donut tube 13, a first supply tube 14, a first mixed gas nozzle 11, and a second mixed gas nozzle 12. The first donut tube 13 is disposed in the cylindrical container 30 so as to correspond to the horizontal cross-sectional shape.

The first supply pipe 14 is connected to the partial oxidation burner 40 and is installed through the wall of the container 30, and connects the first donut pipe 13 to the inner end, so that the solid carbon produced by the partial oxidation The hot syngas containing solid carbon may be supplied into the first donut tube 13 and the vessel 30.

The first donut tube body 13 includes first and second mixed gas nozzles 11 and 12 for injecting a mixed gas. The first and second mixed gas nozzles 11 and 12 form an injection direction at angles θ1 and θ2 set inward and outward with respect to the reference line BL1 in the vertical direction in the first donut tube body 13. The reference line BL1 is set in the first donut tube 13 through a cross section in the vertical direction, that is, a center in the vertical direction in the vertical direction.

The first and second mixed gas nozzles 11 and 12 contain solid carbon supplied from the partial oxidation burner 40 via the first supply pipe 14 and the first donut pipe 13. The high temperature synthesis gas is injected at the set angles θ1 and θ2 in the inner and outer directions of the first donut tube body 13. The angles θ1 and θ2 are set to 90 degrees or less with respect to the reference line BL1. That is, the angles θ1 and θ2 prevent high temperature syngas from being injected upward in the container 30.

The first and second mixed gas nozzles 11 and 12 are respectively installed inside and outside the center line at the bottom of the first donut tube body 13 to uniformly inject the syngas into the container 30 so that the first donut tube body From below (13), hot syngas can be uniformly sprayed onto the dropped caulked catalyst C1 at angles θ1 and θ2 set to the inside and the outside.

The injected hot syngas is mixed with the caulked catalyst (C1) falling from the catalyst inlet (31), and the caulked catalyst (C1) is the first distance (L1) between the first and second nozzle assemblies (10, 20) Caulking additionally via). That is, the catalyst falling into the second nozzle assembly 20 via the first distance L1 is the catalyst C2 further coked by a high temperature synthesis gas containing solid carbon.

The second nozzle assembly 20 includes a second donut tube 23, a second supply tube 24, a first air nozzle 21, and a second air nozzle 22. The second donut tube 23 is disposed in the cylindrical container 30 and formed to correspond to the horizontal cross-sectional shape.

The second supply pipe 24 is installed through the wall of the container 30, and connects the second donut pipe 23 to the inner end to supply hot air to the second donut pipe 23 and the inside of the container 30. Can be supplied as

The second donut tube body 23 includes first and second air nozzles 21 and 22 for blowing hot air. The 1st, 2nd air nozzles 21 and 22 form the injection direction in the 2nd donut tube body 23 with the angle (theta) 3 and (theta) 4 set inward and outward with respect to the reference line BL2 of the up-down direction. The reference line BL2 is set in the second donut tube body 23 through a vertical cross section, that is, a circle through a center in the vertical direction.

The first and second air nozzles 21 and 22 carry hot air supplied through the second supply pipe 24 and the second donut pipe 23 to the inside and the outside of the second donut pipe 23. Spray at the set angle (θ3, θ4). Angles (theta) 3 and (theta) 4 are set to 90 degrees or less with respect to reference line BL2. That is, the angles θ3 and θ4 prevent hot air from being blown upward in the container 30.

The first and second air nozzles 21 and 22 are respectively installed inside and outside the center line at the bottom of the second donut tube body 23, so that the hot air is uniformly injected into the container 30, so that the second donut tube body Under (23), hot air can be uniformly sprayed on the additionally caulked catalyst C2 which is further caulked at angles θ3 and θ4 set inward and outward.

The injected hot air is mixed with the additionally coked catalyst C2 falling via the first nozzle assembly 10 and the first distance L1, and the further coked catalyst C2 is added to the second nozzle assembly 20. ) Is regenerated by hot air via the second distance L2 between the catalyst outlet 32 and the catalyst outlet 32. That is, the coke attached to the additionally coked catalyst (C2) is burned by hot air while passing through the second distance (L2).

Via the second distance L2 region of the vessel 30, the regenerated catalyst C3 is discharged to the catalyst outlet 32 of the vessel 30 and supplied back to the riser connected to the catalyst outlet 32. It is mixed with naphtha and used for the decomposition reaction of naphtha.

Hereinafter, various embodiments of the present invention will be described. Compared with the first embodiment and the previously described embodiment, the same configuration will be omitted and different configurations will be described.

5 is a cross-sectional view of the (first, second) supply unit applied to the catalyst regenerator according to the second embodiment of the present invention. Referring to FIG. 5, in the catalyst regenerator 2 according to the second embodiment, at least one of the first supply part and the second supply part is formed of a supply pipe 51 connected to an outer circumferential side of the container 30.

The supply pipe 51 may be directly connected to the outer circumference of the container 30 and applied to the first supply part and the second supply part. When used as the first supply part, the supply pipe 51 supplies a synthesis gas containing solid carbon into the container 30 to further coke the coked catalyst. When used as the second supply, the supply pipe 51 supplies hot air into the vessel 30 to regenerate the additional coked catalyst. The supply pipe 51 simplifies the supply structure of the syngas and the hot air.

6 is a cross-sectional view of the (first, second) supply unit applied to the catalyst regenerator according to the third embodiment of the present invention. Referring to FIG. 6, in the catalyst regenerator 3 according to the third embodiment, at least one of the first supply part and the second supply part includes a supply chamber 62 and a supply pipe 61.

The supply chamber 62 is formed along the outer circumference of the container 30 so as to be connected to the supply port 34 formed in the container 30. The supply pipe 61 is connected to the supply chamber 62 to the outside. The supply pipe 61 and the supply chamber 62 may be connected to the outer circumference of the container 30 and applied to the first supply part and the second supply part.

When used as the first supply part, the supply pipe 61, the supply chamber 62, and the supply port 34 supply the syngas containing solid carbon into the container 30 to further coke the caulked catalyst. When used as the second feed, feed tube 61 and feed chamber 62 and feed port 34 supply hot air into vessel 30 to regenerate the additional coked catalyst. The supply chamber 62 and the supply pipe 61 make it possible to uniformly supply syngas and hot air in the circumferential direction of the container 30.

7 is a sectional view of a catalyst regenerator according to a fourth embodiment of the present invention. Referring to FIG. 7, in the catalyst regenerator 4 according to the fourth embodiment, the vessel 70 includes a catalyst inlet 71 for introducing a caulked catalyst and a catalyst outlet 72 for discharging the regenerated catalyst. . The first supply unit 73 supplies a synthesis gas containing solid carbon to the caulked catalyst introduced into the catalyst inlet 71. The second supply part 74 supplies hot air into the container 70.

The catalyst inlet 71 may be provided above the vessel 70, and the catalyst outlet 72 may be provided below or to the side of the vessel 70. For convenience, in FIG. 7, the catalyst outlet 72 is provided on the side of the vessel 70.

As an example, the catalyst inlet 71 includes a plurality of catalyst pipes 71 arranged long downward in the interior of the vessel 70 to guide the inflow of the caulked catalyst. In this case, the catalyst outlet 72 is formed on the side of the vessel 70 at a position ΔH higher than the lower end of the catalyst pipe 71. The height difference ΔH thus prevents the caulked catalyst from being discharged into the catalyst outlet 72 without being regenerated in the vessel 70.

The first supply portion 73 is formed on the side of the vessel 70 at a lower position than the lower end of the catalyst pipe 71, and supplies a high temperature synthesis gas containing solid carbon into the vessel 70 to add a caulked catalyst. Caulk. The second supply portion 74 is formed below the vessel 70 at a lower position than the first supply portion 73 to supply hot air to regenerate the additional coked catalyst.

8 is a block diagram of a flow catalyst cracking reaction system according to an embodiment of the present invention. Referring to FIG. 8, a fluid catalytic cracking (FCC) reaction system of one embodiment includes a reaction unit 100, a separation unit 200, and a catalyst regenerator 300.

The reaction unit 100 generates a reaction product (eg, olefin) by causing a decomposition reaction by mixing a catalyst with a target material (eg, naphtha) to be supplied. For example, the reaction unit 100 performs a refinery process for separating various kinds of oil from petroleum, a process for producing olefins from naphtha, propane dehydrogenation (PDH), and the like.

Separation unit 200 separates the reaction product generated in the reaction unit 100 with the catalyst caulked during the decomposition reaction according to the properties and characteristics. For example, the separation unit 200 may include a separation device (not shown) or a cyclone 210 to separate the reaction product and the caulked catalyst after the decomposition reaction. The reaction product is fed to the next process, and the caulked catalyst is fed to the catalyst regenerator 300 below.

The catalyst regenerator 300 is configured as described with reference to FIGS. 1 to 4, and regenerates the caulked catalyst flowing into the catalyst inlet 31 from the separation unit 200, and through the catalyst outlet 32, the reaction unit ( Feed back to 100). To this end, the catalyst inlet 31 of the catalyst regenerator 300 is connected to the separation unit 200, the catalyst outlet 32 is connected to the reaction unit 100.

9 is a flowchart of a catalyst regeneration method according to an embodiment of the present invention. Referring again to the catalyst regeneration method with reference to Figure 9, the catalyst regeneration method according to an embodiment of the catalyst supply step (ST1) for supplying the coked catalyst, the additional coking step for additional coking the coked catalyst with a high temperature synthesis gas (ST2), a regeneration step (ST3) for regenerating the further coked catalyst, and a discharge step (ST4) for discharging the regenerated catalyst.

That is, the caulked catalyst supplied in the catalyst supplying step is further coked in the additional coking step, moving further from the top of the catalyst regenerator 300, and further coked, regenerated in the regenerating step, and regenerated after the discharge step. It is discharged via diesel.

The catalyst supply step ST1 feeds the coked catalyst from the fluid catalytic cracking (FCC) reaction system to the vessel 30 of the catalyst regenerator 300. The catalyst supply step ST1 supplies the coked catalyst to the catalyst inlet 31 provided above the vessel 30.

An additional coking step ST2 is further coked by supplying hot syngas containing solid carbon to the first nozzle assembly 10 to the coked catalyst in the vessel 30. The regeneration step ST3 supplies hot air to the third nozzle assembly 20 to regenerate the additional coked catalyst.

Discharge step ST4 discharges the additional coked catalyst through the catalyst outlet 32 provided below the vessel (30). The additional caulked catalyst is fed back to the reaction section 100 to catalyze.

Although the preferred embodiments of the present invention have been described above, the present invention is not limited thereto, and various modifications and changes can be made within the scope of the claims and the detailed description of the invention and the accompanying drawings. Naturally, it belongs to the range of.

The scope of the present invention is not limited to the above-described embodiments and modifications, but may be embodied in various forms of embodiments within the scope of the appended claims. Without departing from the gist of the invention claimed in the claims, it is intended that any person skilled in the art to which the present invention pertains falls within the scope of the claims described in the present invention to various extents which can be modified.

Description of the sign

1, 2, 3, 4, 300: catalyst regenerator 10: first nozzle assembly

11: first mixed gas nozzle 12: second mixed gas nozzle

13, 23: 1st, 2nd donut tube 14, 24: 1st, 2nd supply tube

20: second nozzle assembly 21, 22: first, second air nozzle

30, 70: vessel 31: catalyst inlet

32, 72: catalyst outlet 33: distributor

34: supply port 40: partial oxidation burner

51, 61: supply pipe 62: supply chamber

71: catalyst inlet (catalyst pipe) 73, 74: first, second supply

100: reaction part 200: separation part

BL1: baseline BL2: baseline

C1: Caulked Catalyst C2: Further Caulked Catalyst

C3: regenerated catalyst L1, L2: first and second distances

Tb: time that can be burned Tm: time that can be blended

Vc, Vcc: Flow velocity θ1, θ2, θ3, θ4: Angle

Claims (20)

1. A container having a catalyst inlet through which the coked catalyst is introduced and a catalyst outlet through which the regenerated catalyst is discharged;

   A first supply unit formed below the catalyst inlet port and supplying a synthesis gas containing solid carbon to the caulked catalyst introduced into the vessel; And

   A second supply part formed below the first supply part and supplying hot air into the container

   Catalyst regenerator comprising a.
2. The method of claim 1,

   The catalyst inlet is disposed above the vessel,

   The catalyst outlet is disposed below the vessel.
3. The method of claim 2,

   The first supply unit

   A first nozzle assembly for supplying the syngas;

   The second supply unit

   And a second nozzle assembly for supplying the hot air.
4. The method of claim 3,

   The second nozzle assembly is

   Spaced apart from the first nozzle assembly and the first distance (L1), spaced apart from the catalyst outlet and the second distance (L2),

   The first distance (L1) is

   The flow rate (Vc) of the caulked catalyst

   Time (Tm) that coked catalyst and hot syngas can mix

   Catalyst regenerator set to the product size of (L1 = Vc * Tm).
5. The method of claim 4, wherein

   The container

   Setting a caulking volume corresponding to the first distance L1;

   The caulking volume is

   A catalyst regenerator is set to a size that can additionally coke the caulked catalyst by the syngas.
6. The method of claim 4, wherein

   The second distance L2 is

   Additionally the flow rate (Vcc) of the caulked catalyst

   The time (Tb) that the additionally coked catalyst can be combusted by the syngas

   Catalyst regenerator set to the product size of (L2 = Vcc * Tb).
7. The method of claim 6,

   The container

   Set a combustion volume corresponding to the second distance (L2),

   The combustion volume is

   And a catalyst regenerator that is set to a size that can additionally burn the caulked catalyst with hot air.
8. The method of claim 3,

   The first nozzle assembly is

   A first donut tube corresponding to the horizontal cross-sectional shape of the cylinder of the container, and

   A first supply pipe installed in the container and connected to the first donut pipe to supply a synthesis gas,

   The first donut tube is

   A catalyst regenerator comprising a first mixed gas nozzle and a second mixed gas nozzle forming a spraying direction at an angle set at 90 degrees or less with respect to a reference line passing through a center in the vertical direction in a circular cross section in the vertical direction.
9. The method of claim 3,

   The second nozzle assembly is

   A second donut tube corresponding to the horizontal cross-sectional shape of the cylinder of the container, and

   A second supply tube installed in the container and connected to the second donut tube to supply hot air;

   The second donut tube is

   A catalyst regenerator comprising a first air nozzle and a second air nozzle forming a spraying direction at an angle set to 90 degrees or less with respect to a reference line passing through a center in the vertical direction in a circular cross section in the vertical direction.
10. The method of claim 1,

    The first supply unit

    A catalyst regenerator connected to a plasma burner that forms a rotating arc to produce syngas in a partial oxidation reaction.
11. The method of claim 1,

    At least one of the first supply unit and the second supply unit

    Catalyst regenerator comprising a supply pipe connected to the outer peripheral side of the vessel.
12. The method of claim 1,

    At least one of the first supply unit and the second supply unit

    A supply chamber formed along an outer circumference of the container and connected to a supply port formed in the container, and

    Catalytic regenerator comprising a supply pipe connected to the outside from the supply chamber.
13. The method of claim 1,

    The catalyst inlet is

    Disposed above the container,

    The catalyst outlet is

    A catalyst regenerator disposed on the side of the vessel.
14. The method of claim 13,

    The catalyst inlet is

    A plurality of catalyst pipes arranged downwardly in the interior of the vessel to guide the inflow of the caulked catalyst,

    The catalyst outlet is

    And a catalyst regenerator formed at a position higher than a lower end of the catalyst pipe.
15. The method of claim 14,

    The first supply unit

    Formed on the side of the vessel at a lower position than the lower end of the catalyst pipe,

    The second supply unit

    And a catalyst regenerator formed below the vessel at a position lower than the first supply portion.
16. Reaction unit for causing a decomposition reaction by mixing the catalyst in petroleum or naphtha;

    A separation unit separating the reaction product generated in the reaction unit from the catalyst according to the properties and characteristics; And

    The catalyst regenerator according to claim 1, which regenerates the caulked catalyst introduced from the separation unit and supplies it to the reaction unit.

    Flow catalyst cracking reaction system comprising a.
17. A catalyst supplying step of supplying a caulked catalyst;

    An additional coking step of further coking the caulked catalyst with hot syngas;

    A regeneration step of regenerating the further coked catalyst; And

    Discharge stage to discharge regenerated catalyst

    Catalyst regeneration method comprising a.
18. The method of claim 17,

    The additional caulking step

    A method for regenerating a catalyst in which a high temperature syngas containing solid carbon is fed to a coked catalyst for further coking.
19. The method of claim 17,

    The regeneration step

    A catalyst regeneration method for regenerating additional coked catalyst by supplying hot air.
20. The method of claim 17,

    The caulked catalyst supplied in the catalyst feeding step is

    A method for regenerating a catalyst via said additional coking step, said regeneration step, and said discharge step while moving from above to below.

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